Process fob making combttstibls gas



Jam, 12, 19:32. w. w. ODELL 1,841,201

PROCESS FOR MAKING COHBUSTIBLE GAS Original Filed Ilalrch' L 1927 q I r k 14 $411M Wade/4.

Patented Jan. 1'2, 1932 1 UNITED STATESPATENT ore ice I WILLIAM W. ODEIEL, OF NEW YORK, N. Y, MANAGEMENT CORPORATION, OF NEW PROCESS FOR MAKING COIBUS TIBI IE GAS ASSIGNOB} 1'0 COLUMBIA ENGINEERING YORK, N. Y., A CORPORATION 03' OHIO bons.

Original application filed March 4, 1927, Serial No. 172,736. Divided and this application filed Kay 8, 1980.

Serial No. 0,797.

This invention relates to a process which consists in generating combustible g s containing hydrogen and carbonmorlilqgde, usparaffin mg one or more hydrocarbons of t at least series as a fuel for the generation of a part of it; natural gas being a ready and low priced source of supply of said hydrocar- An important part of the process is based upon the chemical reactions occurring when the paraflin hydrocarbons are subjected to the action of heat, i. e., when they are caused to contact heated surfaces, particularly in the presence of steam; the contactmg surface may be carbonaceous or other substances.

An object of my invention is to-utilize economically the parafiin hydrocarbons which, in the natural-gas fields are so frequently wasted. v

Another object "of my invention is to produce a gas, using said hydrocarbons, which will have the right proportional amounts of (CO) and hydrogen (H carbon monoxide for the synthetic production of methanol, i. e.,

. about 2 parts of H to one part of CO, since the methanol reaction is represented by the equation,

- standard 1 oo+2H2=oiaoH Further objects of my invention are to provide a flexible means of producing gas of quality using paraflin hydrocarbons, in chemical reactions, in the generation of a partthereof; to produce water gas with -.higher eificiency and at a lower cost than when using. solid fuel alone, by the use of said hydrocarbons in chemical reaction; to

a use gaseous hydrocarbons in substantially the pure state or in simple mixtures, and to increase the gas making capacity of the generator of a 'carburettedwatengas set.

It should be noted that with the advent of the new and improved oil-cracking processes in oil refining practice so much of the low- I density hydrocarbons is formed that a limit has been put upon the amount of the latter which can be present in natural-gas gasoline used in blending; and .this has resulted, in very recent months, in the availability of large quantities of C H (LH and C,H

which can be obtained either in a high degree of purity or mixed with each other or with methane.- The propane (C H and butane ((1 11 are now wasted to a large extent by being burned in pilots in some of the natural-gas fields, even in' those fields where the methane and ethane are piped to centres of consumption.

I find it possible to produce hydrogen and .carbon monoxide, using the paraflin hydrocarbons, at a lower cost than when using solid fuel only at nominal prices. I also find that this gas canbe enriched with hydrocarbons at a lower cost than that of ordinary carburetted water gas.

The chemical equations of interest and which are alluded to hereinafter are as follows:

'In the above there are two classes of reactions; Equations 2 to 5 inclusive show the effect of completely cracking the parafiins by the application of heat; and equations 6 to 9 inclusive show the efiect of beating them in the presence of sufficient steam to combine with the carbon by the water-gas reaction as shown in Equation 10. It is obvious then that in the generation of the ideal water-gas ((10+i-I mixturef) using paraiiin hydrocarbons there is a pre erred proportion of steam and carbon to be used with the latter. In common practice in generating water-gas a much larger amount of steam is necessarily used than enters into the chemical reaction and this will hold true in this instance. This ratio can be varied at will within certain limits; E nation 6 shows the conditions for a ratio 0 3 ml and the other equations show smaller ratios; that in Equation 10 in which is 'tpractically no upper-limit ratio short of in nity when reactions 2 to are considered. The latter reactions do not represent efiicient gasification and are not of themselves new.

The process of making water gas- (CO and ((3 11 andbutane (C H yield a gas, by

reactions represented in Equations 8 and 9,. which is quite satisfactory for the production of methanol (CI-LOH). Thus it is apparent that the reaction shown in Equation 10, commonly known as the water-gas reaction, need not enter into or become a part of the reaction producing a mixture of H and CO- other than in the conversion of the carbon of hydrocarbons to CO. In other words, additional carbon is not necessary. Also it is to be noted that the gas generated is substantially free from suspended carbon thereby making it unnecessary to treat the gas for the removal of carbon.

The apparatus in which I am able gas by m process panying rawing, ront elevation of to make a suitable gas generator i set, with portions of the shells cut away to show the interior in section for clearness.

The enerator is shown connected with douc ble c ecker chambers such as the carburetor and superheater'of a carburetted water-gas set, but obviously it can function without the latter.

In the drawing, 1 is the gas having door 2 for placing soli rial shown at 4, and supported as enerator shell, contact mateat v3. The

- steam supplyv line is shown'at 5, having inlet control valves for us and down run steam respectively at 6 an 7. isrsuppliedto the generator t ough sup lyline 8, having inlet control valves 9 an 10. The ofitakes for finished gas are shown at 11, 11', 12 and 12', and the respective control valves are shown at 13, 13', 14 and 14. Air is supplied through inlet 15 and control valve 16., The l checker chambers 17 and 18 are so connected that gas from 13 and 14: can be passed through them and out through ofitakes 21 and 22 by controlling valves 23 and 24. A connection for hydrocarbon gas is shown at 19 with control valve 20. Checkerbrick or contact material is shown at 25 and introduced through 26 and a steam control valve at 27 for introducing steam into chamber 18. Secondary air is admitted through 28 and 29, and enriching oil or other carburetting material, is

30 and 31. A steam inlet=for cooling back-flow gas and valves is shown at 35. One procedure for operating descence b is shown in the accom-. in which the figure 1s a.

-reaching chambers 17 Hygrocarbon gas by my process for the production of. combustible gas, in cycles is as follows: Referring to the drawing, the checker work is blasted with ignited by rocarbon fuel and air to incanopening valve 16 and admitting air throug lfi while injecting hydrocarbon through 10. The air blast gases, when they contain combustible matter, may be burned in chambers 17 and 18 by introducing air through 28 and 29 and then dischar ed through 21 and-23. The air blasting is s continued, valve 16 is closed, cap 23 is closed and valves 6 and 24 are opened, valves 13 and 10 remaining open, and a regular hydrocarbon gas and steam run is made. Either alternate up and down runs are made or splitruns are made during the steaming periodsone air-blasting and one steaming perio making a complete cycle. The cycles are repeated. When ordinary down runs are valves 6, 10, 13 and 13 are closed and made, I

7, 9 and 14 are opened.- During the valves admission of steam during the up-runs, hy--' run, by operating valve 10. In t is manner solid fuel is not consumed in the generator during the steam-run periods and less heat energy is used per thousand cubic feet of gas made, than in generating water gas in the ordinary mannerfrom solid fuel. carbon gas may be introduced durin up-run, durin both up and own runs, or duringa' certain predetermined ercentage of the total number of runs. hen steam only is passed through generator 1, it is superheated before and 18. Further it cleans up any deposit of carbon lodged in the checker work in 1. It will be apparent that there are conditions when a straight The hydro- -each steam 'runvis desired, not only for the superheating of steam subsequently used in the enriching chambers, but also for the double purpose of cleaning up carbon and maintaining aproper distribution of heat in the primary generator 1. Furthermore, an excess of h drocarbon gas may be used, that is, beyon the normal end of the run period. In the latter period the gas is not appreciably cracked and functions chiefly as a heatcarrying agent, helping to equalize the temperature in generatorl, and to carburetfthe make gas. When a mixture of paraflin hydrocarbons are introduced into the generator 1, as through 10. during a prolonged part of an up-run, of the series are appreciably cracked. .In

this manner the amountof cracking and the I a portion of each run. uringthe higher members only I a study of the equations will reveal. It apgas to determine whether or pears that not only is the capacity of the generator increased when reformin gas, and the gasification efliciency raised a ove that of normal water-gas practice, but the overall efficiency in 'makingreformed and carburetted reformed gas and emplo ing hydrocarbon gas as described is hig er. than other processes using hydrocarbons, such as the combined oil gas reformed gas process and the like, so far as I am aware.

So far, the use of hydrocarbon gas on the up-runs only, has been discussed. It can be and is used when desired on the down-runs as well. Means are provided for introducing the hydrocarbon gas through Valve 20 and inlet 19, and steam through 27. In this manner the gas, and preferably, the steam also are preheated before reaching the reaction zones by heat energy otherwise wasted. In fact a considerable amount of reactions 6, 7, 8 and 9 takes place in the checker chambers 17 and 18 before reaching generator 1. To a large extent the amount of carbon formed during the run when operating in the manner described above is controlled by varying the proportions of steam and hydrocarbon gas used. -When using a large roportion of hydrocarbon gas there is a ten ency for some carbon to form and deposit in the checker work. Increasing the steam and hydrocarbon gas ratio reduces this deposit to a minimum.

In the generation of gas for use in manufacturing synthetic met anol, when the proportion of CO and H must be held within fixed limits andwhen the latter gases are preferred to the exclusion of other gases, it is necessary to operate with generator temperatures well above the dissociation or reaction temperatures; this is provided for by adjusting the amount of air used with respect to the steam and hydrocarbon gas used; short cycles are used under these conditions. After the generator is in operation it is only necessary to analyze the generated not the cycle should be changed and whether the air,

. steam and hydrocarbon gas are properly proportioned. For example, with insufii-. cient air blasting (heating of the checker work during the heating period) or its equivalent, too much steam and h drocarbon gas, the percentage of CO and OH, in the generated gas increases. With suflicient air blasting, the OO content of thegenerated gas increases as the ratio steam to h dro- 5 carbon gas increases. Should it be desirable to materiall increase the content of H beyond that s own in Equations 6 to 10 it is only necessary to materially reduce the amount of steam used and allow reactions 2 to 5 to take place according to the hydrocarbon used.

The paraflins are not the only hydrocarbon gases which can be used in the production of mixed CO and H by chemical reaction with steam; they are mentioned in particular because. they are commercially available in large quantities. Ethylene (C H,) a byproduct in the cracking of petroleum in the manufacture of gasoline is also a suitable hydrocarbon-for the purpose, as shown by the following equations:

(11) C H upon heat crackin 55C 2H One way of converting 0 H, into methanol is shown by Equations 12 and 1. It will be noted that in Equation 12 the gas formed has the right proportionof CO and H for Equation 1, hence for the latter purpose, when using (3 H in the generator, t is desirable to so operate that the generated gas is substantially as shown in Equation 12. One of the fundamentals of my process, then, consists in causing steam and hydrocarbon gas to be introduced simultaneously into an incandescent mass of solids, which mass may or may not comprise coal, coke or the like,

and causing said steam and gas to react chemi- Y I -cally in definite proportions which are substantially and at least one molecule of H,O for every carbon atom present in the reacting hydrocarbon gas. The complete cycleof operation,' using a multi le-shell set, as shown in the drawing, and using hydrocarbon gason both the up and down runs is substantially as follows U blast the generator 1 with air and a combustible heating gas until the checker bricks are incandescent, meanwhile conducting the blast gas into the attached checker chambers 17 and 18, burning its combustible matter therein by the addition of secondary air admitted through 29 and causing the burned gas to pass. out of said chambers through 23; discontinuing the air-blasting and introducing both steam and hydrocarbon gas into generator 1 through 6 and 10 9, and removing the reaction products from the preferred ofltakes and causing them to pass through the checker chambers 17 and 18, discontinuing this steam and hydrocarbon gas run and repeating the cycle, except. that the subsequent run is made as follows: Steam and hydrocarbon gas are introduced into the top of the superheater 18 in substantially molecular proportions, caused to react at least in part in chambers 17 and 18nd conducted into the generator 1 fizleferably from above the checkers, the 'shed gas being removed from beneath them through 12' and 14. Obviously, in-

stead ofmaking alternate up and down runs,

v the selectedor desired percentages of carbon process being less than 50 When sufiicient hydrocarbon as is available,"

' I prefer monoxide and hydrogen in the finished gas, aswell as for reasons already given.

When it is intended to use the gas made as city-gas, enricher may be added to generated gas flowin through the checker chambers 17 and .18 ore sewhere. If oil is used as enricher, it can be cracked more efficiently in the atmosphere of CO+H than in the oil-gas process; the efiiciency of gasification in thzgatter percent., w ereas with the same gas oil the gasifica 11 efficiency in the cracking of said oil in an atmosphere of CO+H is 70 percent. or more.

to enrich the 00+ 2 mixture by introducing the former into the latter in the checker chamber 17. A special inlet for it is not shown for simplicity, since about the same result is obtained by opening valve 9 on the up runs and valve 10 on the down runs.

' This method of introducing the enricher tends to keep valves 13 and 14 0001.

There are conditions and localities in this country where it-is necessary to alter the gas making process used in generating city gas because of a variation in the supply of natural gas and variation in demand for gas.

I believe I have a flexible unit which may be subjected to'cons'iderable variation in operation without materially altering the quality of the finished gas. For example, in the apparatus shown in the drawing, water-gas 0 1-211 can be made in the generator 1 almost entirely from hydrocarbon gas, such as natural gas, and enriched with natural gas when the supply of the latter is suflicient to meet the demand. On the other hand, when this supply is low, the CO and H mixture can be made in the generator essentially from other fuel, using the natural gas for enriching only; in extreme cases the enriching can in part be done by introducing gas oil into the checker chambers, as in the standard carburetted water-gas process. It may be done by introducing hydrocarbon gas through 10 or 9 on up and down runs respectively during the latter part of the steam run, or after the steam-gas runs.

In making straight CO and H mixtures, containing only small percentages of other gases. from hydrocarbon gas as a base raw material, or from both hydrocarbon gas andother fuel, the temperature of the checker bricks in chambers 17 and 18- should be ap' preciably higher than is common practice in making carburetted water-gas. The temperature should beypreferably above 1700 de-- quent cycle is made by factory. When gas oil is used and a carburetted gas, such as city gas, is made, lower temperatures are more satisfactory, namely, 1400 to 1550 degrees Fahrenheit. The latter is also true when carburetting by introducing hydrocarbon gas into the gas entering checker chambers 17 and 18 from the generator.

Coal, coke or the like, is a satisfactory filler for generator 1 and is a splendid contact medium for carrying on reactions as represented by Equations 2' to 12 inclusive, but for the reactions represented by Equations 2 to 9 inelusive, and 11 and 12, solid fuel is not essential; a hot refractory surface is satisfactory as shown in the drawing.

Referring again to the drawing, when it is desirable not to completely crack all of the hydrocarbon gas used in the process, and yet to maintain high temperatures in the chambers 17 and 18, the operation may be so conducted that the gas produced in the generator does not pass through chambers 17 and 18. In this manner the checker bricks in the latter chambers can be used to full advantage for producing carbon monoxide and hydrogen from steam and hydrocarbon gas by admitting the latter materials respectively through 27 and 20. The complete operation is as follows: first, air-blast and burn a gaseous fuel in 1, conducting blast gas into checker chambers 17 and 18, through 13, simultaneously admitting secondar air to 17 through 28 for combustion of the blast gas, discharging the products of combustion through 21 and 23. Now discontinue the air blasting, close stack 23 and introduce steam through 6 and hydrocarbon gas through 10, taking the resulting ting hydrocarbon gas to generator through 9 also when enriched gas is desired. A subsefirst air-blasting as just described and then, when the checker bricks in the different chambers are sufiiciently hot, discontinuing the air-blasting, closing stack 23, introducing steam and bydrocarbon gas simultaneously through 27 and 20 respectively, causing them to react chemi-' cally during their passage through 18 and 1 7, conducting the reaction products and any excess of either gas or steam or both out of 17 through the generator 1 and out of generator; the latter step may consist in passing the gaseous products from 17 through 13 and 11, down through the checkers and out through 12 and 14', or, when 13 is closed, through 14, up throughthe checkers in 1 and out through 13. When said gaseous roducts from 17 are passing through cham er 1, either upwardly or downwardly, additional steam may be introduced therein simultaneously with them by opening respectively valves 6 and 7. When suflicient hydrocarbon product off through 13', admitgas is available it also may be introduced into introduciiig steam therewith in amount sufligenerator 1 along with the steam and the gaseousproducts from 17 by opening valve before up runs and valve 9 before down runs. Furthermore, when the enriching is done with hydrocarbon gas, both valves 9 and 10 are open during up and down runs, the excompose the hydrocarbon gas, simultaneously.

tent of enriching in this instance depending upon the relative amounts of hydrocarbon gas used in the reactions and introduced after the products have emerged from the contact mass.

My gas-generating apparatus is so designed that a substantially constant quality of gas can be made therein, using varying relative amounts of steam and hydrocarbon gas in the process. The temperatures in the checker chambers 17 and 18 are maintained by the combustion of blast gas therein, but when necessary or desired additional gas'is supplied thereto by opening valve 9 during the upward air blasting of the generator fuel. Finished gas can be taken from gen.- erator through ofitakes and valves at top and bottom (above and below the contactmass) as shown at 13 and 14', besides the ofi'takes leading through the checker chambers.

I usually operate at temperatures such that the higher hydrocarbons are reformed to lower hydrocarbons, hydrogen and carbon monoxide.

In the following claims the term checker material is intended to be inclusive of any mass of solid refractory material, porous to passage of the gas therethrough, and which offers the contact surface and intimacy of contact required for the high temperaturegas reactions resulting in the formation of carbon monoxide and hydrogen.

This application is a division of my copending application Serial No. 172,736, filed March 4, 1927, now Patent No, 1,762,100.

I claim: 1. A. process of generating gas which gas is substantially free from suspended carbon resulting from hydrocarbon decomposition, which consists in introducing hydrocarbon gas into amass of non-combustible checker material heated to a degree sufficient to decompose the hydrocarbon gas, simultaneously introducing steam therewith in amount sufficient to effect substantially complete reaction with the hydrocarbon gas, thereby producin a gas comprisingessentially hydrogen an carbon monoxide and in which the ratio of hydrogen to carbon monoxide is substantially from two to one tothree to one.

2. A process of generating gas which gas is substantially free from suspended carbon resulting from hydrocarbon decomposition, which consists in introducing hydrocarbon gas into a mass of non-combustible checker material heated to a degree suflicient to decient to e ect substantially com lete reaction with the hydrocarbon gas, there y producin a ggis comprising essentially hydrogen and car on monoxide and in which the ratio of hydrogen to carbon monoxide is substantially two to one.

' 3. A process of generating gas which gas is substantially free from suspended carbon resulting from hydrocarbon decomposition, which consists in introducing hydrocarbon gas of the paraflin series into a mass of noncombustible checker material heated to a degree suflicient to decompose the hydrocarbon gas, simultaneously introducing steam therewith in amount sufiicient to effect substantially com lete reaction with the hydrocarbon gas, there y producin a as comprising essentially hydrogen an ear n monoxide and in which the ratio of hydrogen to carbon monoxide is substantially from two to one to three to one.-

4. A process of generating gas which gas is substantially free from suspended carbon resulting from hydrocarbon decomposition, which consists in introducing hydrocarbon gas of the paralfin series into a mass of noncombustible checker material heated to a degree suificient to decompose the hydrocarbon gas, simultaneously introducin steam therewith in amount sufiicient to e ect substantially complete reaction with the hydrocarbon gas, thereby producing gas comprising essentially hydrogen and carbon monoxide and in which the ratio of hydrogen to carbon monoxide is substantially two to one.

5. A process of generating gas which gas is substantially free from suspended carbon resulting from hydrocarbon decomposition, which consists in introducing h drocarbongas into a mass of non-combusti le checker materialheated to a degree suflicient to decompose the hydrocarbon gas and to a temperature suflicient for a water gas reaction to occur, simultaneously introducing steam therewith in amount suflicient to effect substantially complete reaction with said hydrocarbon gas' and simultaneous reaction with carbon in thesaid mass-of fuel to'the extent that the resulting gas comprises hydrogen and carbon monoxide in the ratio of substantially two to one. a

6. A process of generating gas which gas is substantially free from suspended carbon resulting from hydrocarbon decomposition, which consists in introducing hydrocarbon gas of the parafiin series into a mass of noncombustible checker material heated to a degree suflicient to decompose the hydrocarbon gas and to a. temperature sufiicient fora water gas reaction to occur, simultaneously introducing steam therewith in amount suflicient to effect substantially complete reaction with said hydrocarbon gas and simultaneous reaction with carbon in the said.

checker material to the extent that the resulting gas comprises hydrogen and carbon monoxide in the ratio of substantially two to one.

7. A process of generating gas which gas is substantially free from sus ended carbon resulting from hydrocarbon ecomposition, which consists in introducing hydrocarbon gas into a mass of non-combustible checker material heated to a degree sufiicient to decompose the hydrocarbon gas, simultaneously introducin steam therewith in amount suificient to e ect substantially complete reaction with the hydrocarbon gas, thereby producing a gas comprising essentially hydrogen and carbon monoxide and in which the ratio of hydrogen to carbon monoxide is substantially from two to one to three-to one, introducin into a stream of the hot gas thus generate gaseous hydrocarbons in amount suiticient to produce an enriched gas being substantially city gas.

8. A process of generating gas'which is substantially free from suspended carbon resulting from hydrocarbon :decomposition, which consists in introducing hydrocarbon gas into a mass of non-combustible checker material heated to a degree suflicient to decompose the hydrocarbon gas, simultaneously introducin steam therewith in amount sufiicient to e ect substantially complete reaction with the hydrocarbon gas,'thereby producing a gas comprising essentially hydrogen and carbon monoxide and in which the ratio of hydrogen to carbon monoxide is substantially two to one, introducing into a streamv of the hot gas thus generated gaseous hydrocarbons in amount suflicient to produce an enriched gas being substantially city gas.

saturated hydrocarbons consisting in, first heating a bed of non-combustible refractory solid material retained in a suitable as generator by blasting it with air and com ustible fluid until it is heated well above the temperature of decompositionof unsaturated hydrocarbons, discontinuing the heating operation and introducing into said bed of refractory both steam and hydrocarbons in a gaseous state controlling the relative amounts of each to maintain the said hydrogen-carbon monoxide ratio,-finally when the temperature is no longer high enough for continued gas generating the gas-making stage is discontinued and the cycle repeated.

10. A process of generating gas which gas is substantially free from suspended carbon resulting from hydrocarbon decomposition, which comprises introducing a gaseous hyhydrocarbon,

9. The process of generating a combustible refractory retained in drocarbon into a mass of non-combustible checker material heated to a degree suflicient to decompose substantial amounts of said simultaneously introducing steam therewith in an amount sufficient to react with a substantial amount of said hydrocarbon,'thereby producing a gas the major portion of which is hydrogen and carbon monoxide and in which the ratio of the h .drogen to carbon monoxide is substantially from two to one to three to one.

11. In a process of making combustible gas intermittently, comprising largely hydrogen and carbon monoxide, using gaseous hydrocarbons as a gas making material, which comprises first heating a mass of non-combustible refractory solids retained in a gas generator to a temperature above 1800 F;, discontinuing the heating operation and then introduc ing into said mass of solids proportioned g5 amounts of steam and a gaseous hydrocarbon, causing them to react chemically forming said combustible gas, removing the latter gas from said generator as formed, said combustible gas being substantially free from suspended on carbon resulting from the hydrocarbon decomposition.

12. A process of making combustible gas intermittently, comprising largely hydrogen and carbon monoxide, using gaseous hydro- 9:

carbons as a gas making material which comprises first heating a mass of non-combustible vrefractory solids retained in an upright gas generator to a temperature above 1800 F.,

discontinuing the heating operation, and then 1' introducing into the heated mass proportioned amounts of steam and gaseous hydrocarbons, causing them to reactchemically with substantially complete reformation of the hydrocarbon, forming said combustible 1 gas, removing the latter gas from said generator as formed, said combustible gas being substantially free from suspended carbon resulting from hydrocarbon decomposition.

13. The process of intermittently making 1 combustible gas, in which 'a gaseous hydrocarbon from the cracking of petroleum in the manufacture of gasoline is used as a gasmaking material, and which gas is substantially free from suspended carbon and con- 1 tains'hydrogen and carbon monoxide in the ratio of at least two to one, which comprises first heating a mass of solid, non-combustible a generator, to a temperature above 1800 F., discontinuing the 1 heating operation and then introducing into said mass of heated refractory proportioned amounts of steam and said gaseous hydrocarbon and causing them to react chemically with substantially complete reformation of 3 said gaseous hydrocarbon and the formation of said combustible. gas by allowing suificient time of contact for reactions to occur, and removing the latter gas from said generator as formed.

14:. A process of making combustible gas intermittently, and in cycles using gaseous hydrocarbons as a gas making material, which comprises heating a bed of non-combustible refractory solids retained in the generator to a temperature above 1800 F., discontinuing the heating operation, introducing into said mass of heated refractory pro-' portioned amounts of both steam and gaseous hydrocarbons, causing said steam and said hydrocarbons to react chemically making a reformed gas substantially free from suspended carbon resulting from the hydrocar- 

